CN117466457B - Continuous flow anaerobic ammonia oxidation denitrification dephosphorization device and method based on granular sludge - Google Patents
Continuous flow anaerobic ammonia oxidation denitrification dephosphorization device and method based on granular sludge Download PDFInfo
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- 239000010802 sludge Substances 0.000 title claims abstract description 181
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 60
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 30
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 27
- 238000000034 method Methods 0.000 title claims abstract description 26
- 230000003647 oxidation Effects 0.000 title claims abstract description 26
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 44
- 238000005842 biochemical reaction Methods 0.000 claims abstract description 31
- 238000004062 sedimentation Methods 0.000 claims abstract description 29
- 239000010865 sewage Substances 0.000 claims abstract description 19
- 238000005273 aeration Methods 0.000 claims abstract description 7
- 238000000926 separation method Methods 0.000 claims abstract description 5
- 238000010992 reflux Methods 0.000 claims description 24
- 238000006243 chemical reaction Methods 0.000 claims description 14
- 239000007789 gas Substances 0.000 claims description 12
- 230000014759 maintenance of location Effects 0.000 claims description 12
- 239000011259 mixed solution Substances 0.000 claims description 10
- 239000002253 acid Substances 0.000 claims description 7
- 230000008569 process Effects 0.000 claims description 7
- LPXPTNMVRIOKMN-UHFFFAOYSA-M sodium nitrite Chemical compound [Na+].[O-]N=O LPXPTNMVRIOKMN-UHFFFAOYSA-M 0.000 claims description 6
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 claims description 4
- 230000001105 regulatory effect Effects 0.000 claims description 4
- 238000003756 stirring Methods 0.000 claims description 4
- 230000010718 Oxidation Activity Effects 0.000 claims description 3
- 239000003513 alkali Substances 0.000 claims description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 3
- 230000033116 oxidation-reduction process Effects 0.000 claims description 3
- 229910052760 oxygen Inorganic materials 0.000 claims description 3
- 239000001301 oxygen Substances 0.000 claims description 3
- 235000010288 sodium nitrite Nutrition 0.000 claims description 3
- 238000011081 inoculation Methods 0.000 claims description 2
- BHEPBYXIRTUNPN-UHFFFAOYSA-N hydridophosphorus(.) (triplet) Chemical compound [PH] BHEPBYXIRTUNPN-UHFFFAOYSA-N 0.000 claims 1
- 229910052799 carbon Inorganic materials 0.000 abstract description 17
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 14
- 238000005265 energy consumption Methods 0.000 abstract description 4
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 17
- 229910052698 phosphorus Inorganic materials 0.000 description 17
- 239000011574 phosphorus Substances 0.000 description 17
- 229920013639 polyalphaolefin Polymers 0.000 description 10
- 241000894006 Bacteria Species 0.000 description 7
- 238000000855 fermentation Methods 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 6
- 230000000694 effects Effects 0.000 description 5
- IOVCWXUNBOPUCH-UHFFFAOYSA-N Nitrous acid Chemical compound ON=O IOVCWXUNBOPUCH-UHFFFAOYSA-N 0.000 description 3
- JVMRPSJZNHXORP-UHFFFAOYSA-N ON=O.ON=O.ON=O.N Chemical compound ON=O.ON=O.ON=O.N JVMRPSJZNHXORP-UHFFFAOYSA-N 0.000 description 3
- 241000408013 Tetrasphaera Species 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 3
- 230000004151 fermentation Effects 0.000 description 3
- 238000012360 testing method Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 208000037534 Progressive hemifacial atrophy Diseases 0.000 description 2
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 2
- 238000012017 passive hemagglutination assay Methods 0.000 description 2
- 229920000903 polyhydroxyalkanoate Polymers 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 229910002651 NO3 Inorganic materials 0.000 description 1
- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 238000013019 agitation Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000000969 carrier Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 238000005469 granulation Methods 0.000 description 1
- 230000003179 granulation Effects 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 230000009935 nitrosation Effects 0.000 description 1
- 238000007034 nitrosation reaction Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
Classifications
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/02—Biological treatment
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/105—Phosphorus compounds
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- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/04—Flow arrangements
- C02F2301/043—Treatment of partial or bypass streams
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
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- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
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- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/308—Biological phosphorus removal
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Abstract
The invention provides a continuous flow anaerobic ammonia oxidation denitrification dephosphorization device and method based on granular sludge. The device comprises a raw water tank, a biochemical reaction tank, a secondary sedimentation tank, a micro-filter and a sludge treatment tank; the method comprises the following steps: s1, inoculating activated sludge of a town sewage treatment plant to a biochemical reaction tank, and inoculating anaerobic ammoxidation granular sludge to an aerobic zone; s2, urban sewage and granular sludge enter an anaerobic zone and then react with floc sludge in a deep anaerobic zone and an aerobic zone; then enters a secondary sedimentation tank for mud-water separation; s3, separating the precipitated sludge of the secondary sedimentation tank into granular sludge and flocculated sludge by a micro-filter; the granular sludge flows back to the anaerobic zone; the flocculated sludge is divided into three parts, wherein the first part enters the sludge treatment tank and then enters the deep anaerobic zone, the second part enters the deep anaerobic zone, and the third part is regarded as the discharge of the residual sludge. The invention reduces the dependence of biological dephosphorization on organic matters in the organic carbon source sewage, and can save aeration energy consumption, thereby realizing low-carbon deep denitrification and dephosphorization of urban sewage.
Description
Technical Field
The invention relates to the technical field of sewage biological treatment, in particular to a continuous flow anaerobic ammonia oxidation denitrification dephosphorization device and method based on granular sludge.
Background
The traditional A2O (Anaerobic-Anoxic-Oxic Anaerobic-anoxic-aerobic) process is a common process for denitrification and dephosphorization of urban sewage, and achieves the aim of denitrification and dephosphorization by the phosphorus release reaction in an Anaerobic zone, the denitrification reaction in an anoxic zone and the nitrification and phosphorus absorption reaction in an aerobic zone. The traditional biological treatment technology has the problems of high operation energy consumption, large emission of greenhouse gases, addition of additional carbon sources and the like.
Short-cut nitrification anaerobic ammonia oxidation is a novel biological denitrification technology process with great development potential, short-cut nitrification means that nitrosation bacteria (NOB) immediately stop after converting ammonia nitrogen into nitrite nitrogen, and the nitrite nitrogen is not converted into nitrate nitrogen, then anaerobic ammonia oxidation reaction is carried out, and the anaerobic ammonia oxidation bacteria convert the nitrite nitrogen and ammonia nitrogen in sewage simultaneously, so that the effect of removing total nitrogen is achieved. The short-cut nitrification anaerobic ammonia oxidation denitrification technology can cut down 100% denitrification carbon source of a sewage treatment plant, and meanwhile, the aeration energy consumption is saved. Therefore, the short-cut nitrification anaerobic ammonia oxidation technology is the technology which has the most prospect for realizing the dual purposes of energy conservation and emission reduction of urban sewage treatment at present.
In the traditional biological phosphorus removal system, the system is very sensitive to the C/N ratio, and the content of organic matters in urban sewage in China is generally low, so that phosphorus accumulating bacteria (PAOs) release phosphorus in an anaerobic zone to cause that the PAOs absorb phosphorus in a subsequent aerobic zone or anoxic zone to a small extent, and the biological phosphorus removal effect cannot reach the national standard; the Tetrasphaera (dephosphorization bacteria) is subjected to deep anaerobic fermentation to produce acid, and then the fermentation product is utilized to carry out dephosphorization in an anaerobic zone and an aerobic zone, so that the problem of insufficient carbon source in raw water in the biological dephosphorization process can be effectively solved, and the requirement on the carbon source in the raw water is reduced; the PAOs utilize fermentation products to store internal carbon sources, promote the anaerobic phosphorus release of the PAOs, and help the subsequent PAOs to fully exert the aerobic excessive phosphorus absorption reaction, thereby realizing the low-carbon deep phosphorus removal effect.
Disclosure of Invention
Aiming at the problem that urban sewage in China generally faces the shortage of organic carbon sources, the invention provides a continuous flow anaerobic ammonia oxidation denitrification and dephosphorization device and method based on granular sludge.
The technical scheme of the invention is realized as follows:
A continuous flow anaerobic ammonia oxidation denitrification dephosphorization method based on granular sludge adopts a continuous flow anaerobic ammonia oxidation denitrification dephosphorization device based on granular sludge, wherein the device comprises a raw water tank, a biochemical reaction tank, a secondary sedimentation tank, a micro-filter and a sludge treatment tank; the biochemical reaction tank comprises 7 cells, wherein the first cell and the second cell are anaerobic areas according to the water flow direction, the third cell is a deep anaerobic area, the fourth cell, the fifth cell, the sixth cell and the seventh cell are aerobic areas, and overflow holes are arranged in an up-and-down staggered manner according to the water flow direction and are connected with the cells; the method comprises the following steps:
S1, inoculating activated sludge of a town sewage treatment plant to a biochemical reaction tank, and inoculating anaerobic ammonia oxidation granular sludge with good anaerobic ammonia oxidation activity to an aerobic zone;
S2, running a device system to enable municipal sewage in a raw water tank and granular sludge returned by a micro-filter to enter an anaerobic zone to form a sludge mixed solution for reaction, enabling the sludge mixed solution and returned floc sludge to enter a deep anaerobic zone for reaction after the reaction is finished, and then enabling the sludge mixed solution and returned floc sludge to enter an aerobic zone for reaction; then the wastewater enters a secondary sedimentation tank for mud-water separation;
S3, separating the precipitated sludge separated by the secondary sedimentation tank into granular sludge and flocculated sludge by a micro-filter; the granular sludge flows back to the anaerobic zone; the flocculated sludge is divided into three parts by the micro-filter, wherein the first part of flocculated sludge enters the sludge treatment tank and then enters the deep anaerobic zone, the second part of flocculated sludge enters the deep anaerobic zone, and the third part of flocculated sludge is regarded as surplus sludge discharge.
Further, the raw water tank is sequentially connected with a biochemical reaction tank, a secondary sedimentation tank and a micro-filter; the outlet of the micro-filter is divided into two pipelines, the first pipeline is connected with the anaerobic zone, the second pipeline is connected with the deep anaerobic zone, a reflux branch pipe and an outer exhaust pipe are arranged on the second pipeline, and the sludge treatment tank is positioned on the reflux branch pipe.
Further, the raw water tank is provided with an overflow pipe and a blow-down pipe; an aeration head is arranged in the aerobic zone and is connected with a gas flow regulating valve, a gas flowmeter and an air compressor in series sequentially through a gas pipeline; the anaerobic zone and the deep anaerobic zone are both provided with a stirrer I; a secondary sedimentation tank water outlet pipe is arranged at the top of the secondary sedimentation tank; the sludge treatment tank is provided with a stirrer II.
Further, a biochemical reaction tank water inlet pump and a biochemical reaction tank water inlet valve are arranged between the raw water tank and the biochemical reaction tank; a secondary sedimentation tank water inlet valve is arranged between the biochemical reaction tank and the secondary sedimentation tank; and a micro-filter mud inlet valve and a micro-filter mud inlet pump are arranged between the secondary sedimentation tank and the micro-filter.
Further, the first pipeline is provided with a granular sludge reflux valve and a granular sludge reflux pump; the second pipeline is provided with a micro-filter mud outlet valve and a micro-filter mud outlet pump and positioned at the front end of the backflow branch pipe and the diversion of the outer calandria, and is provided with a floc sludge backflow valve and positioned at the rear end of the backflow branch pipe and the diversion of the outer calandria; the return branch pipe is provided with a sludge inlet valve of the sludge treatment tank and a sludge outlet valve of the sludge treatment tank and is respectively positioned at two sides of the sludge treatment tank; and the outer drain pipe is provided with a surplus sludge drain valve.
Further, in the step S1, the concentration of the activated sludge in the biochemical reaction tank after the activated sludge is inoculated is 3000-5000mg/L; in the step S1, the concentration of the granular sludge in the aerobic zone after inoculation of the granular sludge is 1000-1500mg/L.
Further, the total hydraulic retention time of the biochemical reaction tank is controlled to be 5.0-12.5 hours; the hydraulic retention time of the anaerobic zone is controlled to be 1.0-1.5h, and the hydraulic retention time of the deep anaerobic zone is controlled to be 2.0-3.0h; the hydraulic retention time of the aerobic zone is controlled to be 2.0-8.0h.
Further, the dissolved oxygen concentration of the aerobic zone is controlled to be 0.3-1.5mg/L by adjusting a gas flowmeter and a gas quantity adjusting valve.
Further, the reflux ratio of the granular sludge in the anaerobic zone is controlled to be 50-110%, and the sludge age of the flocs is controlled to be 6-15d by adjusting the discharge amount of the residual sludge; the reflux ratio of the flocculated sludge in the deep anaerobic zone is controlled to be 50-110%; and when the stirring in the deep anaerobic zone is stopped, the oxidation-reduction potential ORP of the sludge mixed solution is less than-300 mv.
Further, sodium nitrite is put into the sludge treatment tank; the nitrite concentration is controlled to be 200-6000mg/L, the pH value is controlled to be 5.5-6 by adding acid or alkali, and the sludge treatment time is controlled to be 6-24h; the ratio of the second part of floccule sludge reflux quantity to the first part of floccule sludge reflux quantity is 3-5:1.
The technical principle of the invention is as follows:
After the system is started, the municipal sewage and the granular sludge returned by the micro-filter enter an anaerobic zone to form sludge mixed liquor, and PAOs are stored by anaerobic phosphorus release and internal carbon source PHAs; then the sludge mixed liquor and the floccule sludge reflowed by the micro-filter enter a deep anaerobic zone, and deep anaerobic fermentation is carried out to produce acid under the action of Tetrasphaera (dephosphorization bacteria), so that the phosphorus release is further promoted; then the sludge mixed liquor enters an aerobic zone to carry out short-cut nitrification and anaerobic ammonia oxidation to realize denitrification, and PAOs carry out aerobic phosphorus absorption; and then the sludge mixed liquor enters a secondary sedimentation tank for sludge-water separation, the precipitated sludge in the secondary sedimentation tank is separated into granular sludge and flocculated sludge through a micro-filter, the granular sludge flows back to an anaerobic zone, the flocculated sludge is divided into three parts after being acted by the micro-filter, the first part of flocculated sludge enters a sludge treatment tank containing free nitrous acid to inhibit Nitrite Oxidizing Bacteria (NOB) so as to realize short-cut nitrification, and then the first part of flocculated sludge flows back to a deep anaerobic zone through a sludge outlet valve of the free nitrous acid sludge treatment tank and the second part of flocculated sludge, and the third part of flocculated sludge is treated as surplus sludge to be discharged.
Compared with other process technologies, the continuous flow anaerobic ammonia oxidation denitrification and dephosphorization method based on the granular sludge has the following advantages:
1) According to the invention, the micro-filter is adopted to separate and reflux the sludge, and the refluxed granular sludge enters the anaerobic zone, so that limited organic matters in raw water are utilized by the granular sludge, the granulation of the sludge is promoted, and the denitrification and dephosphorization effects are enhanced; the returned floc sludge provides more substrates for deep anaerobic fermentation acid production carbon sources, is beneficial to PAOs to store internal carbon sources PHAs, promotes the growth and formation of granular sludge, and effectively avoids the problem of insufficient organic carbon sources in sewage treatment.
2) Compared with biological membranes, the invention sorts the sludge into granular sludge through the micro-filter without adding biological carriers, thereby saving investment cost; compared with the traditional nitrification and denitrification and short-cut denitrification and anaerobic ammonia oxidation denitrification, the short-cut nitrification and anaerobic ammonia oxidation denitrification can further save aeration energy consumption, and meanwhile, no additional carbon source is needed, so that the operation cost is reduced.
3) Tetrasphaera (phosphorus accumulating bacteria PAOs) performs deep anaerobic fermentation to produce acid, promotes the PAOs to further release phosphorus by utilizing fermentation products, reduces the demand of carbon sources in raw water, reduces the adding amount of phosphorus removing agents, and achieves the effect of low-carbon deep phosphorus removal.
4) The invention reduces the discharge amount of the residual sludge, reduces the disposal cost and reduces the pollution to the environment.
Drawings
FIG. 1 is a schematic structural diagram of a continuous flow anaerobic ammonia oxidation denitrification and dephosphorization device based on granular sludge.
In the figure, a 1-raw water tank, a 2-biochemical reaction tank, a 3-secondary sedimentation tank, a 4-micro filter, a 5-sludge treatment tank, an 11-overflow pipe, a 12 blow-down pipe, a 21-biochemical reaction tank water inlet pump, a 22-biochemical reaction tank water inlet valve, a 23-anaerobic zone, a 24-deep anaerobic zone, a 25-aerobic zone, a 26-stirrer I, a 27-air compressor, a 28-gas flowmeter, a 29-gas flow regulating valve, a 210-aeration head, a 31-secondary sedimentation tank water inlet valve, a 32-secondary sedimentation tank water outlet pipe, a 41-micro filter mud inlet valve, a 42-micro filter mud inlet pump, a 43-micro filter mud outlet valve, a 44-micro filter mud outlet pump, a 45-floc mud reflux valve, a 46-surplus sludge discharge valve, a 47-granular sludge reflux valve, a 48-granular sludge reflux pump, a 51-sludge treatment tank mud inlet valve, a 52-stirrer II and a 53-sludge treatment tank mud outlet valve.
Detailed Description
In order to better understand the technical content of the present invention, the following provides specific examples to further illustrate the present invention.
The experimental methods used in the embodiment of the invention are conventional methods unless otherwise specified.
Materials, reagents, and the like used in the examples of the present invention are commercially available unless otherwise specified.
Example 1
The continuous flow anaerobic ammonia oxidation denitrification dephosphorization method based on the granular sludge adopts a continuous flow anaerobic ammonia oxidation denitrification dephosphorization device based on the granular sludge, and the device comprises a raw water tank 1, a biochemical reaction tank 2, a secondary sedimentation tank 3, a micro-filter 4 and a sludge treatment tank 5; the biochemical reaction tank 2 comprises 7 cells, wherein according to the water flow direction, a first cell and a second cell are anaerobic areas 23, a third cell is a deep anaerobic area 24, a fourth cell, a fifth cell, a sixth cell and a seventh cell are aerobic areas 25, and through holes are arranged up and down in a staggered manner according to the water flow direction and are connected with the cells; the method comprises the following steps:
S1, inoculating activated sludge of a town sewage treatment plant to a biochemical reaction tank 2 to ensure that the concentration of the activated sludge is 4000mg/L; inoculating anaerobic ammonia oxidation granular sludge with good anaerobic ammonia oxidation activity to an aerobic zone 25, so that the granular sludge concentration is 1300mg/L;
S2, running a device system to enable the municipal sewage in the raw water tank 1 and the granular sludge returned by the micro-filter 4 to enter an anaerobic zone 23 to form a sludge mixed solution for reaction, enabling the sludge mixed solution and the returned flocculated sludge to enter a deep anaerobic zone 24 for reaction after the reaction is finished, and then enabling the sludge mixed solution and the returned flocculated sludge to enter an aerobic zone 25 for reaction; then the wastewater enters a secondary sedimentation tank 3 for mud-water separation;
S3, separating the precipitated sludge separated by the secondary sedimentation tank 3 into granular sludge and floc sludge by the micro filter 4; the granular sludge is returned to the anaerobic zone 23; the flocculated sludge is divided into three parts by the micro-filter 4, wherein the first part of flocculated sludge enters the sludge treatment tank 5 and then enters the deep anaerobic zone 24, the second part of flocculated sludge enters the deep anaerobic zone 24, and the third part of flocculated sludge is regarded as surplus sludge to be discharged.
Test conditions
The test adopts artificial water distribution as raw water, and the specific water quality is as follows: COD concentration is 112-240mg/L; NH 4 + -N concentration is 23-38mg/L, NO 2 --N≤0.4mg/L,NO3 - -N is less than or equal to 0.6mg/L, and TP is 1.5-3.2mg/L. As shown in FIG. 1, each reactor is made of organic glass, the effective volume of the biochemical reaction tank 2 is 35L, the biochemical reaction tank is divided into 7 cells, and the volume of the sludge treatment tank 5 is 12L.
After the device system is started, the operation of the operation time adjustment is as follows:
1.1 The total hydraulic retention time of the biochemical reaction tank 2 is controlled to 7 hours, wherein the hydraulic retention time of the anaerobic zone 23 is controlled to 1.0 hour, and the hydraulic retention time of the deep anaerobic zone 24 is controlled to 2 hours; the hydraulic retention time of the aerobic zone 25 is controlled to be 4 hours.
1.2 The reflux ratio of the 23 granular sludge in the anaerobic zone is controlled at 80 percent; the sludge age of the floccules is controlled to be 7.4d by adjusting the discharge amount of the residual sludge;
1.3 Anaerobic zone 23 with continuous agitation; stirring in the deep anaerobic zone 24 for 0.5h, and stopping for 3.5h;
1.4 The floc sludge reflux ratio of the deep anaerobic zone 24 is controlled at 80%; when stirring is stopped, the oxidation-reduction potential ORP of the sludge mixed solution in the deep anaerobic zone 24 is less than-300 mv;
1.5 Controlling the ratio of the reflux amount of the sludge of the second part of the flocs to the reflux amount of the sludge of the first part of the flocs to be 4:1;
1.6 The dissolved oxygen concentration in the aerobic zone 25 is controlled to be 0.3-1.5mg/L;
1.7 Sodium nitrite is added into the free nitrous acid sludge treatment tank 5, the nitrite concentration of the treatment tank is controlled to be 3100mg/L, acid or alkali is added to control the pH value of the treatment tank to be 5.5, and the sludge treatment time is controlled to be 15h.
The test results show that: after the operation is stable, under the condition that no external carbon source is added, the COD concentration of the effluent of the device is 30-60mg/L, and the average COD concentration is 45mg/L; NH 4 + -N concentration is 0-3mg/L, average 1.5mg/L; NO 2 - -N concentration <1mg/L, average 0.5mg/L; the concentration of NO 3 - -N is 0-5mg/L, and the average concentration is 2.5mg/L; TP concentration was <0.5mg/L, and the average was 0.25mg/L.
The foregoing description of the preferred embodiments of the invention is not intended to be limiting, but rather is intended to cover all modifications, equivalents, alternatives, and improvements that fall within the spirit and scope of the invention.
Claims (9)
1. The continuous flow anaerobic ammonia oxidation denitrification and dephosphorization method based on the granular sludge is characterized by adopting a continuous flow anaerobic ammonia oxidation denitrification and dephosphorization device based on the granular sludge, wherein the device comprises a raw water tank (1), a biochemical reaction tank (2), a secondary sedimentation tank (3), a micro-filter (4) and a sludge treatment tank (5); the biochemical reaction tank (2) comprises 7 cells, wherein according to the water flow direction, a first cell and a second cell are anaerobic areas (23), a third cell is a deep anaerobic area (24), fourth, fifth, sixth and seventh cells are aerobic areas (25), and overflow holes are arranged in an up-and-down staggered manner according to the water flow direction and are connected with the cells; the method comprises the following steps:
s1, inoculating activated sludge of a town sewage treatment plant to a biochemical reaction tank (2), and inoculating anaerobic ammonia oxidation granular sludge with good anaerobic ammonia oxidation activity to an aerobic zone (25);
S2, running a device system to enable the municipal sewage in the original water tank (1) and the granular sludge returned by the micro-filter (4) to enter an anaerobic zone (23) to form a sludge mixed solution for reaction, and enabling the sludge mixed solution and the returned flocculated sludge to enter a deep anaerobic zone (24) for reaction after the reaction is finished, and then entering an aerobic zone (25) for reaction; then enters a secondary sedimentation tank (3) for mud-water separation; the total hydraulic retention time of the biochemical reaction tank (2) is controlled to be 5.0-12.5h; the hydraulic retention time of the anaerobic zone (23) is controlled to be 1.0-1.5h, and the hydraulic retention time of the deep anaerobic zone (24) is controlled to be 2.0-3.0h; the hydraulic retention time of the aerobic zone (25) is controlled to be 2.0-8.0h;
S3, separating the precipitated sludge separated by the secondary sedimentation tank (3) into granular sludge and floccule sludge by the micro-filter (4); the granular sludge flows back to the anaerobic zone (23); the flocculated sludge is divided into three parts by a micro-filter (4), wherein the first part of flocculated sludge enters a sludge treatment tank (5) and then enters a deep anaerobic zone (24), the second part of flocculated sludge enters the deep anaerobic zone (24), and the third part of flocculated sludge is regarded as surplus sludge discharge; the reflux ratio of the granular sludge in the anaerobic zone (23) is controlled to be 50-110%; the sludge age of the floccules is controlled to be 6-15d by adjusting the discharge amount of the residual sludge; the reflux ratio of the flocculated sludge in the deep anaerobic zone (24) is controlled to be 50-110%; the ratio of the second part of floccule sludge reflux quantity to the first part of floccule sludge reflux quantity is 3-5:1.
2. The continuous flow anaerobic ammonia oxidation denitrification and dephosphorization method based on granular sludge according to claim 1, wherein the raw water tank (1) is connected with a biochemical reaction tank (2), a secondary sedimentation tank (3) and a micro-filter (4) in sequence; the outlet of the micro-filter (4) is divided into two pipelines, the first pipeline is connected with the anaerobic zone (23), the second pipeline is connected with the deep anaerobic zone (24), a reflux branch pipe and an outer calandria are arranged on the second pipeline, and the sludge treatment tank (5) is positioned on the reflux branch pipe.
3. The method for continuous flow anaerobic ammoxidation denitrification and dephosphorization based on granular sludge according to any one of claims 1 or 2, wherein the raw water tank (1) is provided with an overflow pipe (11) and a blow-down pipe (12); an aeration head (210) is arranged in the aerobic zone (25), and the aeration head (210) is sequentially connected with a gas flow regulating valve (29), a gas flowmeter (28) and an air compressor (27) in series through a gas pipeline; the anaerobic zone (23) and the deep anaerobic zone (24) are both provided with a stirrer I (26); a secondary sedimentation tank water outlet pipe (32) is arranged at the top of the secondary sedimentation tank (3); the sludge treatment tank (5) is provided with a stirrer II (52).
4. The continuous flow anaerobic ammonia oxidation denitrification and dephosphorization method based on granular sludge according to any one of claims 1 or 2, wherein a biochemical reaction tank water inlet pump (21) and a biochemical reaction tank water inlet valve (22) are arranged between the raw water tank (1) and the biochemical reaction tank (2); a secondary sedimentation tank water inlet valve (31) is arranged between the biochemical reaction tank (2) and the secondary sedimentation tank (3); a micro-filter mud inlet valve (41) and a micro-filter mud inlet pump (42) are arranged between the secondary sedimentation tank (3) and the micro-filter (4).
5. The continuous flow anaerobic ammonia oxidation denitrification and dephosphorization method based on granular sludge according to claim 2, wherein the first pipeline is provided with a granular sludge reflux valve (47) and a granular sludge reflux pump (48); the second pipeline is provided with a micro-filter mud outlet valve (43) and a micro-filter mud outlet pump (44) and positioned at the front end of the backflow branch pipe and the diversion of the outer calandria, and the second pipeline is provided with a floc mud backflow valve (45) and positioned at the rear end of the backflow branch pipe and the diversion of the outer calandria; the return branch pipe is provided with a sludge inlet valve (51) of the sludge treatment tank and a sludge outlet valve (53) of the sludge treatment tank and is respectively positioned at two sides of the sludge treatment tank (5); and the outer drain pipe is provided with a surplus sludge drain valve (46).
6. The continuous flow anaerobic ammoxidation denitrification and dephosphorization method based on granular sludge according to claim 1, wherein in step S1, the activated sludge concentration of the biochemical reaction tank (2) after inoculating activated sludge is 3000-5000mg/L; in the step S1, the concentration of the granular sludge in the aerobic zone (25) after inoculation of the granular sludge is 1000-1500mg/L.
7. The continuous flow anaerobic ammoxidation denitrification and dephosphorization process based on granular sludge according to claim 2, wherein the aerobic zone (25) is controlled to have dissolved oxygen concentration of 0.3-1.5mg/L by adjusting gas flow meter (28) and gas flow regulating valve (29).
8. The continuous flow anaerobic ammoxidation denitrification and phosphorous removal process based on granular sludge of claim 1 wherein the sludge mixed liquor oxidation reduction potential ORP < -300mv when the deep anaerobic zone (24) stops stirring.
9. The continuous flow anaerobic ammoxidation denitrification and dephosphorization method based on granular sludge according to claim 1, wherein the sludge treatment tank (5) is fed with sodium nitrite; the nitrite concentration is controlled at 200-6000mg/L, the pH value is controlled at 5.5-6 by adding acid or alkali, and the sludge treatment time is controlled at 6-24h.
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| US20230257290A1 (en) * | 2022-02-14 | 2023-08-17 | Thomas E. Coleman | Process for a batch gravity thickening and fermentation of a mixed liquor |
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| CN108383239A (en) * | 2018-03-13 | 2018-08-10 | 北京工业大学 | The integral biological treatment process of short distance nitration Anammox dephosphorization simultaneously under intermittent aerating pattern |
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